WO2023084035A1 - Cycle de brayton à régénération de dioxyde de carbone supercritique, doté de multiples récupérateurs et compresseurs auxiliaires - Google Patents

Cycle de brayton à régénération de dioxyde de carbone supercritique, doté de multiples récupérateurs et compresseurs auxiliaires Download PDF

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WO2023084035A1
WO2023084035A1 PCT/EP2022/081641 EP2022081641W WO2023084035A1 WO 2023084035 A1 WO2023084035 A1 WO 2023084035A1 EP 2022081641 W EP2022081641 W EP 2022081641W WO 2023084035 A1 WO2023084035 A1 WO 2023084035A1
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stream
recuperator
compressor
mpa
inlet
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PCT/EP2022/081641
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English (en)
Inventor
David NOVALES DE LA PEÑA
Aitor ERCORECA GONZÁLEZ
Iván FLORES ABASCAL
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Universidad Del País Vasco /Euskal Herriko Unibertsitatea
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Publication of WO2023084035A1 publication Critical patent/WO2023084035A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
    • F01K25/10—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours the vapours being cold, e.g. ammonia, carbon dioxide, ether
    • F01K25/103—Carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C1/00—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid
    • F02C1/04—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid the working fluid being heated indirectly
    • F02C1/10—Closed cycles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C7/00—Features, components parts, details or accessories, not provided for in, or of interest apart form groups F02C1/00 - F02C6/00; Air intakes for jet-propulsion plants
    • F02C7/08—Heating air supply before combustion, e.g. by exhaust gases
    • F02C7/10—Heating air supply before combustion, e.g. by exhaust gases by means of regenerative heat-exchangers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B3/00—Other methods of steam generation; Steam boilers not provided for in other groups of this subclass
    • F22B3/08—Other methods of steam generation; Steam boilers not provided for in other groups of this subclass at critical or supercritical pressure values

Definitions

  • the present invention is applicable in the energy industry, for the conversion of heat sources at low-, medium- or high-temperature, which allows generating energy in the turbine with high energy efficiency, said energy being mechanical or electrical energy, in the latter case when the turbine is coupled to an electric generator.
  • Supercritical carbon dioxide regenerative Brayton cycle with multiple recuperators and auxiliary compressors improves the energy efficiency of the conversion of thermal energy from low-, medium- and high-temperature heat sources to mechanical or electrical energy when compared to state-of-the-art regenerative Brayton recompression cycle.
  • the object of the present invention is to improve the energy efficiency of supercritical carbon dioxide recompression cycles of the state-of-the-art through the use of a new cycle configuration that improves the heat recovery process.
  • Any heat source could be used for the cycle, such as heat of solar origin or nuclear origin, heat obtained from the combustion of matter such as fossil fuels, biomasses, waste or biogas, waste heat coming from any process or any other heat source which reaches the temperatures required in the present invention.
  • the first step is to define the optimum number of recuperators N to be installed in the cycle (where N > 3).
  • the optimum number of recuperators in the cycle is calculated as follows.
  • Turbine Inlet (stream Tl according to Figure 1) pressure (P TI ) and temperature (T TI ) and turbine outlet (stream RHIN according to Figure 1) pressure (P RHIN ) are defined.
  • RHI N stands for Recuperator N Hot Inlet, see Figure 1.
  • turbine isentropic efficiency ( ⁇ s, T ) is defined.
  • turbine outlet temperature is obtained using thermophysical properties of CO 2 and turbine isentropic efficiency definition as per equations (1) to (5).
  • h TI stands for the specific enthalpy of stream Tl
  • s TI stands for the specific entropy of stream stands for the specific enthalpy of stream RHIN for an adiabatic and isentropic expansion, stands for the specific enthalpy of stream RHIN.
  • main compressor inlet (stream MCI according to Figure 1) pressure (P in ) and temperature (T in,1 ) are defined.
  • Main compressor inlet pressure shall be the same or lower than turbine outlet pressure (pressure at state RHIN according to Figure 1).
  • Main compressor outlet pressure (P out ) shall be the same or higher than turbine inlet pressure (pressure at state Tl according to Figure 1).
  • T in i stands for the inlet temperature of the i th compressor
  • h in i stands for the inlet specific enthalpy of the i th compressor
  • s inii stands for the inlet specific entropy of the i th compressor
  • h out s i stands for the outlet specific enthalpy of the of the i th compressor for an adiabatic and isentropic compression
  • h out,i stands for the specific enthalpy of the stream leaving the i th compressor
  • T in,1 is defined as the temperature of stream MCI
  • pinch i is defined as the minimum temperature difference between the cold stream and hot stream of the i th recuperator.
  • the optimum number of recuperators N that can be included in the present invention cycle is defined as i-1 , being i the number of the iteration when the stopping criterion (equation 11) is complied with.
  • One main compressor and N-1 auxiliary compressors are associated with those N recuperators according to the configuration shown in Figure 1.
  • the optimum number of recuperators to be included in the cycle is 4.
  • the method for generating energy by means of a multiple recompression cycle using supercritical carbon dioxide (sCO 2 ) as a working fluid comprises the following steps, according to the numbering indicated in Figure 1 :
  • sCO 2 stream at the Recuperator N Cold Outlet is at pressures between 7.5 MPa and 50 MPa and is heated by means of an external heat source to temperatures between 50 °C and 900 °C, reaching stream Turbine Inlet (Tl).
  • sCO 2 stream Tl is expanded in a turbine to a pressure between 3 MPa and 10 MPa (stream Recuperator N Hot Inlet (RH IN)), and generates some mechanical or electrical energy, in the latter case when the turbine is coupled to an electric generator.
  • RH IN stream Recuperator N Hot Inlet
  • sCO 2 stream RH IN is cooled to stream RHON (Recuperator N Hot Outlet) and heats stream RCI N (Recuperator N Cold Inlet) to RCO N in the recuperator number N.
  • sCO 2 stream RH I N-1 is cooled to stream RHO N-1 in recuperator number N-1 and heats stream RCI N-1 to RCO N-1 .
  • Stream RHO N-1 is split into two streams: RH I N-2 and Auxiliary Compressor N-1 Inlet (ACI N-1 ).
  • Stream ACI N-1 is compressed in auxiliary compressor N-1 to, preferably, the pressure of stream RCO N-1 generating the stream ACO N-1 (Auxiliary Compressor N-1 Outlet).
  • Stream ACO N-1 is mixed with stream RCO N-1 , obtaining from the mixture stream RCI N .
  • Stream RH IN-2 is sent to recuperator N-2.
  • step 6) If N>3, the pattern shown in step 5) is repeated for recuperators N-2 to 2.
  • recuperator 1 the sCO 2 stream RHI 1 is cooled to stream RHO1 in recuperator number 1 and heats stream RCI 1 to RCO 1 .
  • Stream RHO1 is split into two streams: Cl (Cooler Inlet) and Auxiliary Compressor 1 Inlet (ACI 1 ).
  • Cl Cooler Inlet
  • ACI 1 Auxiliary Compressor 1 Inlet
  • Stream ACI 1 is compressed in auxiliary compressor 1 to, preferably, the pressure of stream RCO 1 generating the stream ACO1.
  • Stream ACO1 is mixed with stream RCO 1 , obtaining from the mixture stream RCI2.
  • Stream Cl is sent to the Cooler.
  • the split factors (Oj) must ensure a similar heat rate capacity in both streams of each recuperator and a similar pinch value in the hot and cold section of each recuperator.
  • the split factor (Oj) is defined as the ratio of ACIj mass flow rate divided by the total CO2 mass flow being expanded in the turbine (stream Tl).
  • each ACOj stream must be similar to the temperature of the corresponding RCOj stream with which is mixed.
  • the pinch values of all recuperators must be similar between them.
  • sCO 2 stream Cl (Cooler Inlet) is cooled down to a temperature between -10 °C and 70 °C (preferably 32 °C) using any external cooling sink, reaching stream MCI (Main Compressor Inlet).
  • sCO 2 stream MCI is compressed in the main compressor to the same or higher pressure than the one defined for the turbine inlet (stream Tl).
  • the outlet of the main compressor is stream RCI 1 .
  • Stream RCI 1 is heated to stream RCO 1 in recuperator 1 using heat transferred from stream RHI 1 to stream RHO 1 . Then, the stream RCO 1 is mixed with stream ACO1 and the mixture is stream RCI 2 .
  • step 13) Pattern shown in step 13) is repeated for recuperators 2 to N-1.
  • Stream RCI N is heated to stream RCO N in recuperator N by cooling stream RHIN to stream RHO N .
  • the multiple recompression cycle of the invention improves the efficiency of the state- of-the-art recompression cycle, which has only two recuperators and one auxiliary compressor.
  • An example of this increase in efficiency can be seen in Table 1.
  • Figure 2 presents the schematic diagram of the state-of-the-art recompression cycle.
  • Figure 3 represents the Temperature-Thermal Power Exchange diagram within the two recuperators of the Figure 2 recompression cycle for the Table 1 example.
  • the state-of-the-art recompression cycle configuration does not permit a proper heat recovery of the sCO 2 stream leaving the turbine at 548 °C. It only permits heating the high pressure sCO 2 stream up to 506 °C (stream 14 of Figure 2).
  • the separation of the temperature profiles occurs in both recuperators (see Figure 3), but it is more notorious in the high temperature recuperator.
  • the possibility of using at least one intercooling stage in the main compression process is contemplated.
  • the use of one or various intercooling stages in the main compression process reduces the compression work, but it makes the heat recovery process more irreversible, mainly in the high temperature recuperator.
  • the high temperature recuperator needs to exchange more heat when the intercooling is present. Since the heat capacity rate of the hot side stream in the high temperature recuperator is lower than the heat capacity rate of the cold side stream, the additional heat required to be exchanged in the high temperature recuperator, generates a higher temperature difference between the streams in the hot section of this recuperator. Consequently, more irreversibilities are present in the high temperature recuperator and this effect reduces the efficiency of the cycle.
  • the effect of the efficiency increase due to compression work reduction does not always compensate the efficiency reduction due to a worse heat recovery (as shown in Table
  • Table 2 presents the same cycles as Table 1 but including an interceding stage in the main compression process.
  • Table 2 it can be seen that the recompression cycle efficiency is reduced from 53.42% (Table 1) to 52.64% (Table 2) due to the inclusion of the intercooling stage.
  • introducing the same intercooling stage to the present invention cycle permits to increase the thermal efficiency of the cycle from 57.26% (Table 1) to 58.05% (Table 2).
  • the intercooling stage on the present invention can be seen in Figure 6.
  • the proposed strategy of using N recuperators in the cycles of the present invention reduces the inefficiencies of the heat recovery process due to the use of intercooling in the main compression process.
  • the use of at least one intercooling stage in the main compression process reduces the temperature of RCI 1 stream (see Figure 1 and stream 1 of Figure 6) and consequently the RHOi temperature (Figure 1) is also reduced, increasing the total heat recovery while maintaining a similar RCO N stream temperature ( Figure 1). This is obtained by means of the following steps:
  • the main compression process is performed with at least one interceding stage and then steps 1) to 15) are applied to define the multiple recompression cycle.
  • equations (6) to (11) When intercooling is used, the application of equations (6) to (11) has to consider the intercooling effect on the main compression process for the calculation of T out,1 (this is the stream RCI 1 of Figure 1). Since T out,1 with interceding is lower than T out,1 without intercooling, the iterative process of equations (6) to (11) to determine the optimum number of recuperators, may lead to a multiple recompression cycle with more than N recuperators than the cycle without intercooling. Once the optimal number of N recuperators is calculated for the cycle with intercooling using the method explained previously for some specific CO2 conditions and equipment specifications, steps 1) to 15) are applied to define the multiple recompression cycle.
  • FIG. 10 shows the schematic of the multiple recompression cycle obtained from the fulfilment of the steps above for the turbine inlet and outlet conditions presented in Table 4.
  • Figure 11 presents the Temperature-Thermal Power Exchange diagram for the present invention case of Table 4.
  • the efficiency of the multiple recompression cycle is 1.23 points greater than the efficiency of the recompression cycle.
  • the CO2 is expanded to a subcritical pressure of 5.3 MPa and the turbine inlet pressure is increased to 35 MPa to take advantage of heat sources in the form of hot mass flows that require to cool down about 240 °C.
  • the pressure jump available in the turbine allows the CO2 to be cooled through an expansion from 680 °C to 437 °C.
  • Figure 12 presents the diagram of the optimal multiple recompression cycle obtained from the fulfilment of the steps described above for the turbine inlet and outlet conditions presented in Table 5.
  • Figure 13 presents the Temperature-Thermal Power Exchange diagram during the heat recovery process for the present invention case in Table 5.
  • Table 5- Comparison between the recompression cycle and the present invention fora cold sink that allows the CO2 to be cooled to temperatures below the critical temperature and a hot source in the form of a hot mass flow that requires a thermal jump of about 240 °C.
  • reheating is also contemplated for the expansion process of the present invention cycle.
  • the temperature profiles on both sides of the heat source heat exchanger are parallel to each other, meaning that the heat rate capacity of the fluids in both sides of the heat source heat exchanger are similar, the inclusion of the reheating has a negligible effect on the increase of the energy efficiency of the cycle.
  • Figure 1- Schematic diagram of the multiple recompression cycle with N recuperators.
  • Figure 2- Schematic diagram of the state-of-the-art recompression cycle.
  • FIG. 4 EMBODIMENT 1 , schematic diagram of the multiple recompression cycle with four recuperators.
  • Figure 6- EMBODIMENT 2 schematic diagram of the multiple recompression cycle with four recuperators and one intercooling stage.
  • FIG. 7 Temperature - Thermal Power Exchange diagram of the heat recovery process within the four recuperators of the multiple recompression cycle including one intercooling stage for a high temperature heat source.
  • FIG. 8- EMBODIMENT 3 schematic diagram of the multiple recompression cycle with three recuperators.
  • FIG. 10- EMBODIMENT 4 schematic diagram of the multiple recompression cycle with three recuperators and three auxiliary compressors.
  • FIG. 12 EMBODIMENT 5, schematic diagram of the multiple recompression cycle with three recuperators.
  • FIG. 13 Temperature - Thermal Power Exchange diagram of the heat recovery process within the three recuperators of the multiple recompression cycle for a high- temperature heat source and a cold sink that allows the CO2 to be cooled to temperatures below its critical temperature.
  • the invention comprises combinations of several elements which have synergistic effects on the improvement of the energy efficiency and on the use of different heat source temperature ranges.
  • Five embodiments are described below, without these examples being a limitation to the possibilities of combination and application of the inventive concepts described above.
  • Figure 4 shows a highly regenerative Brayton cycle with multiple recuperators and auxiliary compressors driven by a high-temperature heat source stream.
  • the cycle depicted in said Figure 4 is a preferred embodiment of the invention for electric generation by means of a heat source available at high temperature.
  • This preferred embodiment has four recuperators and three auxiliary compressors. It must be noted that, from now on, when making reference to the total sCO 2 mass flow rate, total sCO 2 mass flow being expanded in the turbine is being referred.
  • the high temperature heat source permits to heat up the sCO 2 stream leaving the recuperator 4 (stream 14) up to 680 °C at 20 MPa (stream 15).
  • the stream 15 is expanded in the turbine to 548 °C and about 7.5 MPa (stream 16).
  • Stream 16 enters the hot side of recuperator 4 and is cooled down to 428.5 °C (stream 19) by means of heating stream 10 from 422 °C to 537 °C (stream 14).
  • recuperator 19 is then cooled down in the recuperator 3 to 308 °C (stream 20) by heating stream 7 from 301 .5 °C to 421 .5 °C (stream 8).
  • Auxiliary compressor 3 compresses the 6.4% of the total sCO 2 mass flow rate from about 7.5 MPa and 308 °C to about 20 MPa and 429 °C (stream 9).
  • Stream 9 is mixed with stream 8 to obtain the stream 10 mentioned above.
  • the 93.6% of total sCO 2 mass flow rate goes to the hot side inlet of recuperator 2 at about 7.5 MPa and 308 °C (stream 21).
  • Stream 21 is then cooled down in the recuperator 2 to 191 .5 °C (stream 22) by heating stream 4 from 185.5 °C to 302 °C (stream 5).
  • Auxiliary compressor 2 compresses the 13.2% of the total sCO 2 mass flow rate from about 7.5 MPa and 191.5 °C to about
  • stream 6 20 MPa and 299 °C (stream 6).
  • Stream 6 is mixed with stream 5 to obtain stream 7.
  • the 80.4% of the total sCO 2 mass flow rate goes to the hot side inlet of recuperator 1 at about 7.5 MPa and 191.5 °C (stream 23).
  • Stream 23 is then cooled down in the recuperator 1 to 90 °C (stream 24) by heating stream 1 from 85 °C to 187 °C (stream 2).
  • Auxiliary compressor 1 compresses the 28.8% of the total sCO 2 mass flow rate from about 7.5 MPa and 90 °C to about 20 MPa and 183 °C (stream 3).
  • Stream 3 is mixed with stream 2 to obtain stream 4.
  • the 51 .6% of the total sCO 2 mass flow rate goes to the cooler at about 7.5 MPa and 90 °C (stream 25).
  • Stream 25 is cooled in the cooler from about 90 °C to about 32 °C (stream 26).
  • Stream 26 is compressed in the main compressor from about 32 °C and 7.5 MPa to about 85 °C and 20 MPa (stream 1).
  • This embodiment allows achieving increases up to 3.8 points with respect to the state- of-the-art recompression cycle working with equipment with identical isentropic efficiencies and effectiveness.
  • Said Figure 4 shows a preferred embodiment for the exploitation of a heat source at high temperature.
  • Figure 6 shows a multiple recompression cycle that uses a high temperature heat source with an intermediate cooling stage in the main compression process.
  • the cycle depicted in said Figure 6 is a preferred embodiment of the invention for electric generation by means of a heat source available at high temperature.
  • This preferred embodiment has four recuperators, three auxiliary compressors and one intercooling stage in the main compression process.
  • the high temperature heat source permits to heat up the sCO 2 stream leaving the recuperator 4 (stream 14) up to 680 °C at 20 MPa (stream 15).
  • the stream 15 is expanded in the turbine to 548 °C and about 7.5 MPa (stream 16).
  • Stream 16 enters the hot side of recuperator 4 and is cooled down to 398 °C (stream 19) by means of heating stream 10 from 390 °C to 534 °C (stream 14).
  • Stream 19 is then cooled down in the recuperator 3 to 264 °C (stream 20) by heating stream 7 from 257 °C to 390.5 °C (stream 8).
  • Auxiliary compressor 3 compresses the 8.2% of the total sCO 2 mass flow rate from about 7.5 MPa and 264 °C to about 20 MPa and 380 °C (stream 9). Stream 9 is mixed with stream 8 to obtain stream 10. The 91 .8% of the total sCO 2 mass flow rate goes to the hot side inlet of recuperator 2 at about 7.5 MPa and 264 °C (stream 21).
  • Stream 21 is then cooled down in the recuperator 2 to 150 °C (stream 22) by heating stream 4 from 144 °C to 258 °C (stream 5).
  • Auxiliary compressor 2 compresses the 18.4% of the total sCO 2 mass flow rate from about 7.5 MPa and 150 °C to about 20 MPa and 252 °C (stream 6).
  • Stream 6 is mixed with stream 5 to obtain stream 7.
  • the 73.4% of the total sCO 2 mass flow rate goes to the hot side inlet of recuperator 1 at about 7.5 MPa and 150 °C (stream 23).
  • Stream 23 is then cooled down in the recuperator 1 to 56 °C (stream 24) by heating stream 1 from 52 °C to 146 °C (stream 2).
  • Auxiliary compressor 1 compresses the 29.3% of the total sCO 2 mass flow rate from about 7.5 MPa and 56 °C to about 20 MPa and 140 °C (stream 3).
  • Stream 3 is mixed with stream 2 to obtain stream 4.
  • the 44.1% of the total sCO 2 mass flow rate goes to the cooler about 7.5 MPa and 56 °C (stream 25).
  • Stream 25 is cooled in the cooler from about 56 °C to about 32 °C (stream 26).
  • Stream 26 is compressed in the main compressor 1 from about 32 °C and 7.5 MPa to about 59 °C and 12.25 MPa (stream 27).
  • Stream 27 is cooled to about 40 °C in the intercooler to obtain stream 28.
  • Stream 28 is compressed in main compressor 2 to about 20 MPa and 52 °C (Stream 1). This embodiment allows achieving increases up to 4.6 points with respect to the state- of-the-art recompression cycle without intercooling working with equipment with identical isentropic efficiencies and effectiveness.
  • Figure 6 shows a preferred embodiment for the exploitation of a heat source at high temperature.
  • FIG. 8 depicted in Figure 8 there is a multiple recompression cycle using three recuperators and two auxiliary compressors.
  • the cycle depicted in said Figure 8 is a preferred embodiment of the invention for electric generation by means of a heat source available at medium temperature.
  • the medium temperature heat source permits to heat up the sCO 2 stream leaving the recuperator 3 (stream 14) up to 377 °C at 17 MPa (stream
  • the stream 15 is expanded in the turbine to 289 °C and about 7.5 MPa (stream
  • Stream 16 enters the hot side of recuperator 3 and is cooled down to 240 °C (stream 20) by means of heating stream 7 from 238 °C to 282 °C (stream 14).
  • Stream 20 is then cooled down in the recuperator 2 to 160 °C (stream 22) by heating stream 4 from 156 °C to 236 °C (stream 5).
  • Auxiliary compressor 2 compresses the 16.3% of the total sCO 2 mass flow rate from about 7.5 MPa and 160 °C to about 17 MPa and 246 °C (stream 6).
  • Stream 6 is mixed with stream 5 to obtain stream 7.
  • the 83.7% of the total sCO 2 mass flow rate goes to the hot side inlet of recuperator 1 at about 7.5 MPa and 160 °C (stream 23).
  • Stream 23 is then cooled down in the recuperator 1 to 80 °C (stream 24) by heating stream 1 from 76 °C to 156.5 °C (stream 2).
  • Auxiliary compressor 1 compresses the 32.5% of the total sCO 2 mass flow rate from about 7.5 MPa and 80 °C to about 17 MPa and 155.5 °C (stream 3).
  • Stream 3 is mixed with stream 2 to obtain stream 4.
  • the 51.2% of the total sCO 2 mass flow rate goes to the cooler at about 7.5 MPa and 80 °C (stream 25).
  • Stream 25 is cooled in the cooler from about 80 °C to about 32 °C (stream 26).
  • Stream 26 is compressed in the main compressor from about 32 °C and 7.5 MPa to about 76 °C and 17 MPa (stream 1).
  • Said Figure 8 shows a preferred embodiment for the exploitation of a heat source at medium temperature.
  • the cold outlet temperature of the heat source stream is fixed by the solar field.
  • the selected turbine inlet pressure permits to work with the Heat Transfer Fluid entering the Heat Transfer Fluid Heat Exchanger at about 390 °C (stream HSi) and leaving this exchanger at about 295 °C (stream HS2).
  • FIG. 10 Besides, according to a fourth preferred embodiment depicted in Figure 10, there is a multiple recompression cycle using three recuperators and three auxiliary compressors.
  • the cycle depicted in said Figure 10 is a preferred embodiment of the invention for electric generation by means of a heat source available at low temperature.
  • the low temperature heat source permits to heat up the sCO 2 stream leaving the recuperator 3 (stream 14) up to 85 °C at 8.6 MPa (stream
  • the stream 15 is expanded in the turbine to 73.7 °C and about 7.5 MPa (stream
  • Stream 16 enters the hot side of recuperator 3 and is cooled down to 61.9 °C (stream 20) by means of heating stream 7 from 61.35 °C to 73.05 °C (stream 8).
  • Auxiliary compressor 3 compresses the 15% of the total sCO 2 mass flow rate from about 7.5 MPa and 61.9 °C to about 8.6 MPa and 73.4 °C (stream 9).
  • Stream 9 is mixed with stream 8 to obtain the stream 14 at 73.1 °C and 8.6 MPa.
  • the 85% of the total sCO 2 mass flow rate goes to the hot side inlet of recuperator 2 at about 7.5 MPa and 61.9 °C (stream 21).
  • Stream 21 is then cooled down in the recuperator 2 to 50.4 °C (stream 22) by heating stream 4 from 49.9 °C to 61.3 °C (stream 5).
  • Auxiliary compressor 2 compresses the 20.4% of the total sCO 2 mass flow rate from about 7.5 MPa and 50.4 °C to about 8.6 MPa and 61.5 °C (stream 6).
  • Stream 6 is mixed with stream 5 to obtain stream 7.
  • the 64.6% of the total sCO 2 mass flow rate goes to the hot side inlet of recuperator 1 at about 7.5 MPa and 50.4 °C (stream 23).
  • Stream 23 is then cooled down in the recuperator 1 to 39.8 °C (stream 24) by heating stream 1 from 39.4 °C to 49.8 °C (stream 2).
  • Auxiliary compressor 1 compresses the 33.6% of the total sCO 2 mass flow rate from about 7.5 MPa and 39.8 °C to about 8.6 MPa and 50.0 °C (stream 3).
  • Stream 3 is mixed with stream 2 to obtain the stream 4.
  • the 31.0% of the total sCO 2 mass flow rate goes to the cooler at about 7.5 MPa and 39.8 °C (stream 25).
  • Stream 25 is cooled in the cooler from about 39.8 °C to about 32 °C (stream 26).
  • Stream 26 is compressed in the main compressor from about 32 °C and 7.5 MPa to about 39.4 °C and 8.6 MPa (stream 1).
  • Said Figure 10 shows a preferred embodiment for the exploitation of a heat source at low temperature being the cold outlet temperature of the heat source stream (stream HS2) fixed by the heat source stream cooling requirements.
  • stream HS2 the cold outlet temperature of the heat source stream
  • the selection of 8.6 MPa as the turbine inlet pressure leads to a particular case where there are as many recuperators as auxiliary compressors.
  • FIG. 12 depicted in Figure 12 there is a multiple recompression cycle using three recuperators and two auxiliary compressors.
  • the cycle depicted in said Figure 12 is a preferred embodiment of the invention for electric generation by means of a high-temperature heat source and a cold sink that allows the CO2 to be cooled to temperatures below its critical temperature.
  • This configuration makes it possible to take advantage of hot sources in the form of mass flows or hot streams that must be cooled about 240 °C by expanding the sCO2 from 35 MPa to subcritical pressures of 5.3 MPa.
  • the high temperature heat source permits to heat up the sCO 2 stream leaving the recuperator 3 (stream 14) up to 680 °C at 35 MPa (stream
  • the stream 15 is expanded in the turbine to 437 °C and about 5.3 MPa (stream
  • Stream 16 enters the hot side of recuperator 3 and is cooled down to 391 °C (stream 20) by means of heating stream 7 from 389 °C to 430 °C (stream 14).
  • Stream 20 is then cooled down in the recuperator 2 to 200 °C (stream 22) by heating stream 4 from 189 °C to 381 °C (stream 5).
  • Auxiliary compressor 2 compresses the 20.3% of the total sCO 2 mass flow rate from about 5.3 MPa and 200 °C to about 35 MPa and 420 °C (stream 6).
  • Stream 6 is mixed with stream 5 to obtain stream 7.
  • the 79.7% of the total sCO 2 mass flow rate goes to the hot side inlet of recuperator 1 at about 5.3 MPa and 200 °C (stream 23).
  • Stream 23 is then cooled down in the recuperator 1 to 32 °C (stream 24) by heating stream 1 from 26.5 °C to 186 °C (stream 2).
  • Auxiliary compressor 1 compresses the 25.6% of the total sCO 2 mass flow rate from about 5.3 MPa and 32 °C to about 35 MPa and 197.5 °C (stream 3).
  • Stream 3 is mixed with stream 2 to obtain stream 4.
  • the 54.1 % of the total sCO 2 mass flow rate goes to the cooler at about 5.3 MPa and 32 °C (stream 25).
  • Stream 25 is cooled in the cooler from about 32 °C to about 5 °C (stream 26).
  • Stream 26 is compressed in the main compressor from about 5 °C and 5.3 MPa to about 26.5 °C and 35 MPa (stream 1).
  • Said Figure 12 shows a preferred embodiment for the exploitation of a heat source at high temperature and a cold sink that allows the CO2 to be cooled to temperatures below its critical temperature.
  • the outlet temperature of the hot stream or thermal fluid that works as a heat source would be set at about 460 °C.
  • the selected turbine inlet pressure permits to work with the Heat Transfer Fluid entering the Heat Transfer Fluid Heat Exchanger at about 700 °C (stream HS1) and leaving this exchanger at about 460 °C (stream HS2).

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  • Engineering & Computer Science (AREA)
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  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
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  • Engine Equipment That Uses Special Cycles (AREA)
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Abstract

Procédé de production d'énergie au moyen d'un cycle de Brayton à régénération de dioxyde de carbone supercritique (sCO2), doté de N récupérateurs en série et de N ou N-1 compresseurs auxiliaires, où N ≥ 3. Un nombre supérieur de récupérateurs en série, et un compresseur auxiliaire pour chaque récupérateur, permettent d'améliorer le processus de récupération de chaleur et ainsi le rendement du cycle par rapport aux cycles de l'état de la technique.
PCT/EP2022/081641 2021-11-12 2022-11-11 Cycle de brayton à régénération de dioxyde de carbone supercritique, doté de multiples récupérateurs et compresseurs auxiliaires WO2023084035A1 (fr)

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